Method for converting hydrocarbon oils



June 6, 1944- w. J. DEGNEN ETAL v METHOD FOR CONVERTING HYDROCARBON OILS Filed April 2, 1958 4 Sheets-Sheet l Nu@ M.

.INVENToRs AT1-0R Y 4 Sheets-Sheet 2 June 6, 1944- w. J. DEGNEN ET Al.

METHOD FOR CONVERTING HYDROCARBON OILS Filed April 2, 1958 NNN June s, 1944. w. J. DEGNEN ET AL 2,350,730.

' METHOD FOR CONVERTING HYDROCARBON OILS 4 Sheets-Sheet 4 ATT NEY W. J. DEGNEN ET AL METHOD FOR CONVERTING HYDROCARBON OILS Filed April 2, 1958 June 6, 1944.

Patented June 6, i944 "UNITED STATES PATENT ol-Flfclig yMirrnon non comme maocannon l .William J. Degnen, Cranford, Henry M. Nelly, Jr., Jersey City, and Percival C. Keith, Jr., Peapack, N. J., assignors to The M. W. Kellogg Company,

9 Claims.

' alyst in order to convert the hydrocarbon oil into the desired products. For variouslreasons, the catalyst passes through various stages of eiectiveness with use, eventually requiring reactivation. Thus, during an operation, the catalyst varies in effectiveness so that, for any given catalyst bed, only average eilectiveness is obtained.

One object of our invention is to provide a method of cracking or polymerization in the presence of a catalyst in which the catalytic bed is continuously being removed and reviviiled so that the catalytic bed will remain of substantially v constant effectiveness.

Another object of our. invention is to utilize a catalyst chamber in which heat is supplied to the oil vapors passing therethrough to control the temperature drop through the chamber.

Other and further objects of our invention will appear from the following description.

In the accompanying drawings which form part of the instant specication and are to be read in conjunction therewith and in which like reference numerals are used in Ithe various views: b

Figure 1 is a diagrammatic view of a portion of the apparatus capable of carrying out the process of our'invention.

Figure 2 shows one modification of the revivifying apparatus used in connection with that portion of the apparatus shown in Figure l.

Figure 3 shows another modification of revivifying apparatus capable of being used in connecto indicate like parts New York. N. I., a corporation of Delaware "9 `Application April 2, 1938. Serial No. 199,702

i change in its composition. This is a major advantage over the intermittent processes ofthe prior art in which the products leaving the catalyst chamber may vary in composition. .In an intermittent process, for example, in which hydrocarbon oils are cracked to form gasoline-like hydrocarbons, at the beginning of a cracking period the vapors leaving the reaction chamber may contain from 4 0% to 50% of gasoline, while,

tion with the apparatus shown in Figure `l for carrying out our invention.

Figure 4 is a sectional view of a catalyst contact chamber adapted to be used in carrying out our invention.

Figure 5 is a sectional view taken on 5-5 of Figure 4.

Figure 6 is another modification of a catalyst contact chambercapable of use in carrying out the process of ouririventlon.

Figure '7 is a sectional view takenon the line 1-1 of Figure 6. l

-a line at the end of the cracking period, they may contain as low as 15% to 20% of gasoline.

In the intermittent processes, in order to obtain high cracking per pass, the cracking period must necessarily be short due to the fact that the catalyst activity falls off rapidly. In a continuous process, the cracking per pass may be raised of the catalyst L by increasing the circulation rate per unit of time.

In the intermittent processes, the `oil vapors to be converted pass through the reaction chamber in contact with highly active catalyst only at or near the beginning of a conversion period. During the latter part of the conversion period, the catalyst is progressively decreasing, in activity. In our method of continuously circulating a catalyst in contact with the oil vapors, theaverage composition of the catalyst remains lsubstantially constant andthe oil vapor always contacts catalyst of highest activity at some point in the chamber.

The catalyst being continuously removed from the reaction chamber is continuously reviviiied and recirculatedto the catalyst chamber.

Heat issupplied to the reaction chamber to compensate for the loss of heat during the endothermic reaction oi' cracking. If the apparatus is to be used for polymerization, heat may be removed from the catalyst by a heat exchanging medium to remove the exothermic heat of poly- `merization.

drocarbons.

More particularly referring now to the drawings, the oil to be converted, which maybe of any suitable type, is pumped from tank l by pump 2 through line 3 through heat exchanger 4, in

heat exchange with the :products of the. cracking 5 reaction which pass to the heat exchanger vthrough line 5. The preheated charging stock leaves heat exchanger 4 through line 9. A portion of the charging stock may-loe passed into the fractionating tower 6 through line 1, which is 10 controlled by valve 8, as a control reflux. The fractionating tower 6 may be of any suitable type such as a bubble tray' tower. The cracked products leave heat exchanger 4 through line I8 and pass into the tower 6 at a point below theintrol5 duction of the control reflux through pipe 1. The cracked vapors are cooled by the reflux coursing down the tower and, if desired, the rate of introducingthe control reflux maybe suehthat the cracked vapors may be quenched to any desired temperature.

The remainder of the charging stock passes through pipe I I where it may be joined by reflux condensate from tower 8, being delivered therefrom by pump I2. The preheated oil from pipe suitable type and the charged oil is heated to any suitable cracking temperature preferably between 750 F. and 950 F. or higher in convection heating coil I5 and in radiantly heated tubes I6, the oil being withdrawn from the furnace through transfer pipe i1 for passage into the the base of the chamber is somewhat above atmospheric and is at least sulllciently high to overcome thefrictional resistance to the flow of vapors through vthe catalyst bed and recovery system. When the vapors pass through the re-` -heate'r 34 1 valves 42 and 43 are open and valve 44 is closed. If desired, the vreheater may be partially. orwholly bypassed by opening valve 44.

Vdiyaporsv are withdrawn from the reaction charn erith'y gh4 pipe 45 and pass into llheat,exchange with the inritroduction through pipe I8 into. the fractiona't tower 6.' The cracked vapors are taken off :overhead Vfrom the tower 6 throughpipe 46- and vpassed through condenser 41 in heat exchangev with 'the cooling medium introduced through pipe 48.

The condensate leaves" the' condenser 41 through pipe 49 and is' introduced thereby 'into a. separator 50 from-which a portion of the condensate is withdrawn through pipe 5I and pumped by pump 52 through pipe 53 for introduction into the top of the tower 6 as condensate relux. The noncondensable gases and uncondensed vapors leave the separator through pipe 54 and are compressed by compressor 55, cooled in heat exchanger 56 by'heat exchange with a cool medium introduced through pipe 51. The compressed and cooled products are withdrawn from the heat exchanger 56 through pipe 58 and passed into a separator 59. The condensate from separator 5b is withdrawn therefrom through pipe 66 and pumped by pump 6I into pipe 62 whence aportion passes through pipe 63 into the staseparator IB in which it iS Separated intO vapors 35 4bilizer section of the combined absorber and staand unvaporized oil. Provision may be made at various points in the furnace for introduction of Vsteam into the oil stream. Recycle stockl withdrawn from the fractionating tower i5 may pass into the separator through pipe I8, to act 4 as refluxing medium in this tower. Dry or superheated steam may be delivered vinto the separator through pipe 28 to strip further vaporsfrom unvaporized oil and also aid in effecting the nature of conversion in the catalyst bed. vaporized oil is withdrawn from the separator through pipe 2| and pumped by pump 22 through a heat exchanger 23 which is lsupplied with cooling medium through pipe 24. The' cooled, un-

vaporized oil leaves the cooler 23 through pipe 50 25 and may be passed through pipe 26 controlled l by valve 21, to storage. A portion of the cool, un-

vaporized o il may be returned to the separator through pipe 28, controlled by valve 29, whence it may be delivered through pipe 3|),k controlled by 55 valve 3|, into contact4 with the highly lheated charging stock to control its temperature. A

portion of the unvaporized oil maybe used as refluxing medium by opening valve 32. The

highly heated oil vapors are withdrawn from the 66 separator I8 through pipe 33 and may pass through pipe 34 into furnace 35 for reheating to y the desired temperature, which may be between 900 F. and 1000 F., depending upon the type ofI end product desired and the type of oil being 65 processed. y'I'he reheated vapors are withdrawn from the furnace 35 through pipe 36 and passed into pipe 31 for introduction through pipe 38 into the base of the reaction chamber 39, Since the vapors suppliedto the base of the reaction 70 chamber 39 flow through the bed of catalyst particles in this chamber and then to the cracked vapors recovery system without vintermediate compressionin the procedure specifically illustrated, obviously, the pressure of the vapors in 5 bined absorber and stabilizer tower, passing upwardly countercurrent to the absorption oil. The

absorption menstruum coursing down the absorber tower countercurrent to the gas, absorbs the valuable, heavier, low boiling, normally liquid hydrocarbons from the gas, the dry gas leaving the tower 68 through pipe 18. The rich absorption menstruum withdrawn from the absorber section 68 through pipe 1I passes into the stripping section 12 of the combination tower, whence it is withdrawn from the lower tray through pipe 13 for passage through reboiler 14 and returned through pipe 15 to the base of the stripping section 12. The heat for reboiling is supplied from the hot reflux `condensate in tower 6, being withdrawn therefrom through pipe 10 and pumped by pump 11 through pipe' 18 for passage through the reboiler 14. The reflux condensate is withdrawn from the reboiler 14 through pipe 19, whence a portion may pass through pipe 88 into the tower 6 as an intermediate reflux, by opening valve 8I. The remainder of the reflux condensate from pipe 19 passes through pipe 82, throughheat exchanger 83 into pipe 84, cooling medium being supplied to heat exchanger 83 through pipe 85. The cooled reflux condensate may be passed through pipe I9 by opening valve 86, or may be withdrawn through pipe 81 by opening valve 88' for passage to av cycle stock storagetank for future use.

Cil

pipe 35 into the top of the stabilizer section 03.

The uncondensed vapors and gases are withdrawn from the stabilizer section and passed through pipe 30 into the absorber section 60 for contact with the absorption menstruum along with the gases introduced through pipe 61. Re-

ux condensate from a lower tray of the stabilizer section 33 is withdrawn through pipe 91 for passage through heat exchanger 33 and returned to the bottom of the stabilizer section I9 through pipe 33. In the heat exchanger 03, the reflux condensate Ais reboiled by heat supplied by the hot denuded absorption menstruum which is being withdrawn from the bottom of the stripping section 12 through pipe |00 and pumped by vpump |0| through pipe |02 through heat exchanger 30, being withdrawn therefrom through pipe |03 and passed through cooler |04 through which cooling medium is supplied through pipe |05'. f

The cooled, denuded absorption menstruum leaves the cooler |06' through pipe 09 for'introduction to the top of the absorber section 60. The stabilized gasoline is withdrawn from the stabilizer section I9 through pipe |04 and-is passed through a nal cooler it to which a cooling medium is supplied through pipe |06. The cooled stabilized motor fuel leaves the heat exchanger |05 through pipe |07 andis passed to storage.

We have seen that the heated vapors pass into the reaction chamber 39. In the reaction chamber the heated vapors react to form lighter hydrocarbons in the' presence of a catalyst. The catalyst in our method is of a granular nature such that it can be fed to and withdrawn from the reaction chamber 39 continuously. The fresh catalyst which may be used or catalyst material which has been revivified, is fed through con'- veyor |08 for passage through duct|09 into the catalyst feeding hopper |10. Converter |08 completes the circuit whereby the catalyst particles are continuously and successively moved through the conversion zone, intermediate purging and sealing zone, and regeneration zone, therebyv attaining the circulation of the catalyst at an elevated temperature throughout the process and the continuous production of a high quality gasoline at a substantial uniform rate and of substantial uniform quality. The conveyor |03 is provided with any suitable conveying means I, driven by any suitable means such as an electric motor ||2. The feeding of the catalyst material ||3 from the feeding hopper ||0 is controlled by a cone type valve ||4, provided with hydraulic operating means ||5. The catalyst material passes and the rate of withdrawal are kept the same. The used catalytic material passes into a sealing hopper |23, the discharge of which is controlled bya cone type valve |24, operated by a hydraulic operating mechanism |23. The hydraulic operating mechanisms il! and |23 are adapted to be supplied with hydraulic fluid through pipes and |21. A fluid pump |20 operated by an electric motor |23 supplies the fluid from pipe |30 for' functioning the hydraulic operating mechanisms ||3 and |2l. A timing control mechanism |3| of any suitable type known to the art controls the electric motor |23 so that the cone type valves |'I4 and |24 are intermittently operated to introduce fresh catalytic. material into sealing hopper and to withdraw used catalytic material from sealing hopper |23. An inert gas, such as flue gas,'steam, or the denuded dry gas from 10, if desired, under suitable pressure and at a suitable temperature. is introduced' into manifold |32. A pipe |33, controlled by a valve |34, permits gas from manifold |32 to flow into feeding hopper H0.. The pressure of the gas is from the feeding hopper ||0 through a duct IIS material is withdrawn from the reaction chamber- 30 by a'. rotary bucket type valve |2| operated by an electric motor |22. The motors |20 and |22 may be synchronized so that the rate of feeding such that it is slightly in excess of that existing in the catalyst chamber. The imposition of this pressure in feeding hopper i0 and in upper sealing hopper will effectively prevent leakage outward of the cracked vapors. Any leakage which might occur will be into the reaction chamber 39. The capacity of the discharge hopper |35 is sufficiently greater than the lower sealing hopper |23 so that there will always be a quantity of material present in discharge hopper |35. Thus continuity of feed to the reviviiier is assured. The pressure in feeding hopper H0 may be readily controlled by value |34 which may be automatically controlled by differential pressure controller between the feeding hopper'ilg and the reaction chamber, if desired.

Sealing gas from manifold |32 is also introduced through pipe |36 controlled by valve |37 into the lower sealing hopper |23. By control 38 into the reaction chamber along with the `hoi;v vapors to be reacted in the reaction chamber.

The stripped, used catalyst passes into .the

discharge hopper |35, whence it-passes through duct |31 and is fed by conveyor |33 to the revivifying operation. Sealing gas from manifold |32 passes through'the pipe |39 controlled b'yvalve i' |40 into thedischarge hop'per |35. If it is desired to locate the reviviiier adjacentthe r`e-\' action chamber, the used catalytic material may be withdrawn through duct |4| normally vsealed by a cover plate |42. I I

Any desired rate of catalyst iiow may be obtained by controlling the speed of motors |24 and |22. The timing arrangement' |3|` is so controlled that conetype valves ||4 and I 2'4 are operated with suiicient frequency vto keep a supply of material in feeding hopper and the discharge hopper |23 sufficiently free of material to receive the used catalytic material flowing from the reaction chamber past valve |2|. It will be'obvious, of course, that the conveyors will b e operated at a synchronous speed to keep the upper lscaling hopper I I0 supplied with material and maintain the material in the lower sealtube |46 by a feeeding screw |41 operated by an electric motor Hi8. The conveyor tube |46 and the feeding screw |41 are tapered to cause the catalytic material to pack densely, enabling it, per se, to act as a seal.

The pressure of the sealing gas in the discharge hopper |35 exists throughout the conveyor tube |38 and in feeding hopper |44, so that any leakage will be merely of material inwardly toward the revivier. yThe revivier is of the rotary kiln type in which the catalytic material is contacteds, with a gas which will effectively remove all or some of the carbon absorbed in the process and regenerate the catalyst to active condition. Proceiver |88 through pipe |88 and may be passed. if desired, through a reheater |90 for heat eX- change with a hot medium such as superheated steam or a portion of hot flue gas from duct |84, supplied to heat exchanger through pipeA |9|. The sealing gas may by-pass the reheater |90 through pipe |92,' controlled by valve |93. The

ducer gas reactions enabling a removal of car Y bon by reduction of carbon dioxide 4and steam may be employed, though we prefer to use simple oxidation with air.

In starting the operation of the revivier. air from the air manifold |49 passes throughpipe A |50 through valve |5|, to a burner |52, to which fuel gas is supplied through the pipe |53. The kiln shell |54 is'provided with a ring gear |55 meshing with'the pinion |58 which is driven by withdrawnfrom .the revivier through d uct |84I and passthrough a centrifugal separator |85 for removal of entrained catalytic material a dust; which lis collected in theseparator bottom |88 and removed therefrom by conveyor screw I8 operated by an electric motor |88. I

The clean flue gases leave the separator |85 through duct |69 and may pass through duct |18l to the stack |1| by opening dampers |12 and |13. The heat in the gases resulting from revivitlcationA of the catalyst may. be recovered in partvby passing them through a` flue gas steam generator |15, after which they may pass through duct |18, past damper |11 to the stack |1I. AA portion of the cooled ue gases may be withdrawny through duct |18 by blower |19 and-.passedthroughduct |80 for recirculation totherevivifierftc'control the temperature of the revivicationl I y A compressor I8 supplies yairgtowpipe|48- Afor sealing gas passes from the reheater |90 or from by-pass line |82 into the sealing gas manifold |32. The rotary revivier is mounted at a slight angle, the stationary section |62 being lower than the stationary section |6|, so that the revivied catalytic material passes from the revivifier through duct |94 into a discharge hopper |85. Fresh catalytic material may be added at this point from hopper |96 through duct |91 controlled by valves i 88 and |98'.

The catalytic material which is too ne for recycling passes out with the flue gases of reviviiication and is separated in the separator |85. The revivlfied catalytic material from hopper |95 is fed by screw conveyor |99, which is operated by electric motor 200, into conveyor feeding chamber 20|, from which the catalytic material passes through duct 202 to the fresh catalytic material conveyor tube |08 for carriage by conveyor means to the reaction chamber catalyst feeding hopper ||0.

Referring now to Fig. 3, we have shown use of another means for revivifying the used catalytic material. In this embodiment of our invention. the catalytic revivifying chamber 203 is a verticar chamber which may be operated at a pressure equal to that employed in the reaction chamber. In this modification the 'used catalytic material passing through conveyor tube |38 passes through duct 204 into a feeding hopper 205 provided with a cone type valve 206 and hydraulic operating mechanism 201. A ductv208 connects the feeding hopper 205 with a sealing hopper 208. A rotary bucket type valve 2| 0 operated by a motor 2|| is provided .for passing the catalytic material to be reviviiled into the revivifying chamber 203. 'I'he reviviied catalytic material is withdrawn from the revivifying chamber 203 by bucket type valve 2 2 operated by an electric motor 2| 3, for passage into sealing hopper 2|4. The revivifled catalytic material leaves hopper 2|4 past a cone type valve 2|5. The

cone type valve 2|5 is provided with hydraulic voperating mechanism 2|8. The hydraulic operating mechanisms 201 and 2| 8 are supplied with hydraulic operating fluid through pipes 2|1 and passage to the revivier. .A 'portionSoif;y the` oi revivication may be withdrawnthrojfighpipe |82 and passedthrough cooler '|88Yfr`c'i'inllre's-l sionbycompressor |84 and passage-through pipe: |85 to a sealing gas're'ceiver |88. .'I'he'cooler mayy be. by-passed Aby by-pass/pipe |81 'controlled by valve |88.v The. compressed ilue. gasesj-in'f nue I gas receiver. acts-v as a source 'ofsealinggasfor the sealing gas system. heretofore described.` ".Ihe, i

sealing gas is withdrawn from the iluegas rethe reaction chamber, back to the reviviiier in a continuous circulating path, and the hot vapors to be cracked are continuously passed in contact with the moving stream of catalytic material. The revivifled catalytic material from sealing chamber 2|4 passes the cone type valve 2| 5 for delivery into discharge hopper 220. p

A vibrating screen22l provided with vibratory actuating means 222 screens out the fines which into a lines collecting hopper 223. The re- ,yiviiled screened catalytic material` through duct 224 into a hopper 225 from which it is fed from hopper 221 to the auxiliary hopper 230. Valve 229 is then closed and valve 232 is opened, permitting materiell t pass through duct 23I into the revivifled catalytic material discharge hopper 220. f

The reviviflcation of vthe catalytic material in bodiment using a heated catalytic reaction chamber is shown. In this embodiment, the catalytic material passes through heat eiichangertubes 245 which are provided at their upper ends with funnel-like portions 240, to directthe flowing catalytic material into the tubes 245. Similarly, the outlet sections of the tubes 2&5 are provided with funnel-like sections 2:31, the heating section of the reaction chamber being jacketed by heat insulating material 204, as before.

By way of illustration and not by way of limif tation, a Mid-Continent virgin gas oil was supthe revivier chamber 203 is by oxidation of the carbon and adsorbed heavy hydrocarbons. Air is taken from the atmosphere Ithrough air intake pipe 232' and is compressed by compressor I8I' and delivered through pipe 233 to an air receiver tank 234 which supplies air through pipe |49.

In starting, the valve II is opened'to supply air to the burner |52, to which fuel gas is supplied through pipe It, the hct gases passing through duct 130 into the revivifying chamber 203. .After the chamber is suiliciently heated, valve ISI is closed and valve IBS is opened to permit air to pass through duct |00 into the revivifying chamber. The gases of combustion during the reviviflcation reaction are withdrawn from the revivifying chamber 203 through duct |04, and may be passed-as before through duct to stack lli by opening dampers |12 and 113. If desired, heat from the gases of combustion may be recovered by passing them through duct |14,

through a waste heat boiler |15 and` thence through duct I10 to the flue pipe I1I past damper 111 and damper I13. e

The blower I19 is adapted `to withdraw flue gases through duct I18 for delivery through duct 300, for controlling the temperature of the reviviiication reaction. Flue gas is Withdrawn from duct |10 through pipe i02 for compressionl by` compressor Ist and delivery to the sealing ilue ing the catalytic material to the central passage 231. Tubes 240 extend between sections 235 and 235, as can be readily seen by reference to Figs. 4

and 5.

Vapors introduced through pipe 38 are disa tributed by a manifold 24| and pass upwardly through the catalytic material and through tubes 240, and are withdrawn through pipe 45. The bailles 238 and 239 prevent the catalytic material from clogging the tubes 240. Any suitable heating medium, such as hot gases of combustionl or mercuryvapors or the like, are introduced through duct 242, for passage in heat exchange relation around the exterior of the tubes 240 and central passage 231, and are withdrawn through -tive ease.

plied to tank i as charging stock for the process. The catalytic material was alumina deposited upon silica gel. The reaction temperature main-r tained within the catalyst bed varied from 840 F. at the bottom to 890 F. at the top. 'I'he time in which the catalyst was retained in passing through the chamber was about 8.25 hours. The space velocityduring the operation was 4.28 barrels per hour of charge per ton of catalyst material in the bed. Under these conditions the Iollowing yields were obtained.

Gasoline C4 recovery) The catalyst was continuously revivified. The

gasoline yield from this run is approximately 12% greater than that predicted for a run under similar conditions made in a stationary catalyst bed.

During the revivifying of the catalyst, it was found that the first 50% of the carbonaceous material absorbed is removed by burning with rela- The last half of the carbonaceous material requires ,a considerably longer .time for revivication. In this connection it is to be noted that it is not necessary to remove all of the carbonaceous material from the catalyst, as the removal of a certain `portieri of it will revivify the catalyst to produce good results during the cracking reaction. For example, where the total carbon absorbed in one run amounted to 17% by weighat of the catalyst, it Was :found that a. reduction of the carbon by burning to 7.2% by weight of the catalyst gave a catalytic material which gave favorable results as compared with an operation in .which fresh catalyst was continuously charged. Y

It is believed that from the foregoing description our method will be clear to those skilled in the art. The operation o the apparatus will be understood from the foregoing description. It will be seen that we have accomplished the objects of our invention. We have provided a method of catalytic cracking in which the composition of the oil vapor leaving the catalyst chamber is substantially constant. This enables it to flow directly to the fractionatlng and stabilization equipment without special precaution being taken for periodic changes in its composition. This is not true in the intermittent process in which the gasoline content of the vapors leaving the reaction chamber may vary from 40% to 50% at the start of the cycle. and be as low as 15% to 20% at the end of the cycle.

In order to obtain a very high cracking per pass in the intermittent process the cycles must necessarily be short due to the rapid falling oli of catalyst activity. In our process of` continuous catalytic material replacement, the cracking per pass may be raised by circulating more catalyst per unitv of time. In the intermittent process the vapors contact highly active catalytic material only a short period of time. In our process highly active catalytic material is constantly being supplied so that there is always present in the reaction zone a considerable bed of highly active catalytic material.

Although the apparatus has been described in connection with a process operated under pressure conditions slightly above atmospheric, it may as well be operated at atmospheric pressure or under sub-atmospheric or vacuum conditions.

While a catalytic cracking process has been described-as particularly adapted to the apparatus, it is also suited to other endothermic catalytic reactions such as dehydrogenation of hydrocarbon oils and gases. To adapt the apparatus to exothermic reactions such as catalytic polymerization or synthesis reactions, provision would be made for removing excess heat produced during the reactions.

We supply the heat of reaction continuously during the cracking reaction, to enable us to obtain a high percentage of cracking per pass.

` It is to be understood, of course, that ifdesired,

a non-heated type of reaction chamber may be employed,^and the heat' supplied by high preheat of the cracked vapors.

It will be understood that certain features and sub-combinations are of utility and may be employed without reference to other features and sub-combinations. This is contemplated by and is within the scope of our claims. It is further obvious that various changes may b e made in .details within the scope of our claims without departing from. the spirit of our invention. It is, therefore, to be understood that our invention is not to be limited to the specic details shown and described. y V

Having thus described our invention, what we claim is:

1. In a process for the catalytic conversion of said reaction zone and purging the accumulated catalyst therein of entrained and adsorbed conversion products by circulating an inert gas therethrough, maintaining a body ofspent catalyst particles withdrawn from said intermediate zone v inl contact with an oxygen-containing gas in a 'confined regenerating zone until the catalystis reviviiled, and continuously and successively moving the catalyst particles through said conversion zone, intermediate purging and sealing zone, and regeneration zone thereby attaining the circulation of the catalyst at an elevated temperature throughout the process and the continuous production of a high quality gasoline at a substantial uniform rate and of substantial uniform quality.

3. -In a continuous process for the catalytic conversion of high boiling hydrocarbons to low boiling hydrocarbons within the gasoline boiling range, involving passing the high boiling hydrocarbons' in the' vapor phase through a conversion zone in contact with a body of catalyst particles maintained at a ltemperature suitable for the desir'ed conversion, the improvement which consists in continuously withdrawing used catalyst from the conversion zone during the reaction and continuously replacing catalyst particles thus withdrawn with active catalyst particles, thereby maintaining the volume of catalyst in said zone and-the average activity thereof substantially constant throughout the reaction. maintaining a confined zone containing an accumulation of used catalyst thus withdrawn in proximity to but separate from the conversion zone, and maintaining saidlatter zone under an inert gas pressure greater than the pressure oi said reaction zone and freeing the accumulated catalyst therehydrocarbons by passing the hydrocarbons in the vapor phase through a reaction zone iilled with catalyst granules and maintained at a temperature suitable for the desired conversion, the improvement which consists in withdrawingused catalyst from said zone at suitable intervals during the reaction and replacing catalyst thus with- 'drawn with active catalyst, thereby maintaining the volume of catalyst in said zone and the average activity thereof substantially constant throughout the reaction. and maintaining a confined zone containing a supply of active catalyst and a similar zone containing an accumulation of used catalyst, each respectively associated with the catalyst replacement and withdrawal portions of the reaction zone. under an inert gas pressure greater than the pressure of said reaction zone.

2. In a continuous process tor the catalytic conversion` of high boiling hydrocarbons to low boiling hydrocarbons within the gasoline boiling range, involving passing the high boiling hydrocarbons in the vapor phase through a conversion' zone in contact with particles of a cracking catalyst and maintained at an elevated temperature suitable for the desired conversion, the improvement which consists in withdrawing used catalyst particles-from the yconversion zone during the reaction land replacing catalyst particles thus with drawn with active catalyst particles. thereby maintaining the volume of catalyst in said zone' and the average activity thereof substantially constant throughout the reaction. maintaining in of entrained and adsorbed conversion products by circulating an inert gas therethrough.

4. A proc as dened in claim 2 wherein a hot heat exc proximity to said moving bed to supply endo- Vthermic heat of cracking. A

5. In the method of hydrocarbon oil conversion -in which the conversion to other hydrocarbon compounds of diiferent properties is brought about by pyrolysis in the presence of a solid contact material or agent, the improvement which consists in moving in a column said contact material from a bulk supply through s. conversion chamber, to a receiver therefor, introducing hydrocarbon vapor to be converted adjacent one end oi'said chamber. withdrawing converted products adjacent the other end of said chamber while maintaining said vapor in said chamber at the conversion temperature, supplying hot inert sas at a point below. said vchamber and below the path of said vapors to be converted and at a point above said bulk supply, said gas beingvsupplied at a somewhat greater pressure than that existing in said chamber, whereby leakage oi vapors of conversion from said chamber into either said bulk supply or said receivervis prevented, and withdrawing said gas admixed with said converted products. v

6. lIn a process for the catalytic conversion of p hydrocarbons by passing the hydrocarbons in the a connned intermediate sealing zone containing vapor phase through a reaction zoneiilledy with catalyst granules and maintained at a tempera-,-

nge medium is passed in close' accesso "enember into said buik supply is prevented, withcatalyst from said zone during the reaction and replacing catalyst thus withdrawn with activeV catalyst, thereby maintaining the volume oi catalyst in said zone and the average activity thereof substantially constant throughout the reaction, and maintaining a conned zone containing 4a supply of active catalyst and a similar zone containing an accumulation of used catalyst, each respectively associated with the catalyst replacement and withdrawal portionsl of the reaction zone, `under an inert gas pressure greater than the pressure of .said reaction zone.

7. A process as deiined in claim 2 further characterized by the. step of continually moving the used catalyst from said intermediate purging and sealing zone through a confined 4transfer zone lled with an inert gas to said regeneration zone.

8. The continuous method oi converting aliquid hydrocarbon oil into high quality gasoline bya process comprising catalytic cracking, which method comprises heating said oil to eiiect vaporization thereof and to eiiect superheating of the vapors to aconversion temperature, introducing said superheated vapors into a moving bed of catalyst in a conversion zone, introducing regenerated catalyst into said zone from a bulk supply thereof disposed above the conversion zone and' removing used catalyst `from the bottom ot v said zone thereby continuously maintaining the volume and average catalytic activity oi the bed of catalyst in said zone substantially constant throughout the conversion, withdrawing the used catalyst out of the path of the vapors through o at high temperature and returning said high temperature regenerated catalyst to said liulk-v supply of regenerated catalyst above said conversion zone, introducing an inert gas into said lbull: supply at a somewhat greater pressure than that existing in the conversion chamber whereby leakage of vapors of conversion from said erating said removed catalyst in a separate sone f 45 ply. withdrawing the vaporous products from the troducing said vapors into a moving bed of catalyst particles in a cracking zone. atga pressure above atmospheric and at least suiilciently high to overcome the frictional resistance by said bedto the flow of the vapors therethrough, inj troducing regenerated catalyst particles from a bulk supply thereof disposed above the -cracking zone into said zone and removing used catalyst particles from the bottom of said zone thereby continuously maintaining a bed of catalyst particles of .both substantially constant volume and average catalyticactivity in said zone throughout the conversion, withdrawing used catalyst.

outv of the vpath of flow of the vapors through the cracking zone to a purging and sealing zone,-

reniovingjhydrocarbons entrained with the withdrawn catalyst by passing an inert gas through the latter zone in contact with the catalyst therein at a pressure above atmospheric and sufilciently'high' relative to the pressure maintained in thecmcking zone to eilectively prevent leakagegutward oi reaction vapors from theconversijxnnone to said purging zone, continuously reugeierating said removed catalyst in a separate 'ggsone at high temperature and continuously ref 5 turning said high temperature regenerated cat-` y alyst to said bulksupplyof regenerated catalyst above said conversion zone, introducing an inert gas into said-bulk supply to maintain an.inert l gaseous atmosphere therein 'at a pressure above `at'u'iosphericf and sufllciently hi h relative to the g zone to eiecpressure maintained in the crac tively prevent leakage of reaction vapors outward from the cracking zone to said bulk sup- 

